Description:FIELD OF THE INVENTION
The present invention relates to a method and an apparatus for separating the reusable catalyst from the heel catalyst. More specifically, the present invention relates to a rotating fluidization method and a fluidization column apparatus for separating reusable low coke content catalyst from the heel catalyst having high coke content generated in continuous catalytic reforming (CCR) process based on the particle density gradient.
BACKGROUND OF THE INVENTION
Continuous catalytic reforming (CCR) is a major conversion process that finds wide-scale application in petroleum refining and petrochemical industries. It converts low-octane naphtha to high-octane gasoline blending stock, and produces aromatic concentrates rich in benzene, toluene and xylene. In addition to that, valuable by-products like H2 and liquified petroleum gas are also produced by this process. This process employs Pt/chlorinated alumina-based catalysts which are spherical in shape with a nominal diameter in the range of 1-2 mm, preferably in the range of 1.4-1.8 mm. The catalyst moves in a close loop between the reactor and the regenerator. The coke deposited in the reactor is burnt in the regenerator. Usually, the regenerator is designed to burn the coke content in the range of 0.1-10 wt% on the catalyst. Burning of higher coke content on the catalyst is undesirable as it leads to an excess temperature rise of the catalyst bed which causes the sintering of precious metals on the catalyst.
In the continuous catalytic reforming (CCR) process sometimes part of the catalyst is held up in the bottom and along the wall side of the reactors. This catalyst does not circulate through the reactor and the regenerator. Over a period of time, the coke content builds upon this portion of the catalyst and increases continuously during the operation. This non-circulating high coked catalyst is termed as the heel catalyst. This heel catalyst is unloaded during the maintenance and inspection shutdown. Due to the high coke content on the heel catalyst, it is very difficult to regenerate this catalyst in the CCR regeneration section. Hence, re-loading of this heel catalyst is avoided in the regenerator. Due to this, the heel catalyst is normally sent for precious metal recovery. However, the heel catalyst also contains a substantial amount of low coke content catalyst which can be reused during normal operation. Owing to the high cost of the CCR catalyst laden with precious metals such as Pt, it is necessary to recover this low coke content catalyst from the heel catalyst to reduce the inventory loss in terms of fresh catalyst cost. The remaining heel catalyst having high coke content can then be sent for precious metal recovery.
In US2561396, an improved method of separating solid mixtures comprising particles having different particle sizes is given. The process includes the segregation of finely divided solids in a contacting zone containing a substantially non-transitory mass of solids in relatively coarse particles. These coarse solid particle's size minimum 10 times of the largest particle in finely divided solid particles. The non-transitory particles form interstices by passing gaseous fluids upwardly so that finely divided solids are stratified with respect to their buoyancies throughout contacting zone and solids withdrawing from contacting zone of different sized solid particles.
EP0479343A2 discloses a method for separation of contaminated catalyst from catalyst mixture by density gradient using an inclined vibrating deck grading apparatus with the stream of air forced upwardly through the vibrating deck to suspend the catalyst particle in the gas phase. The particles are suspended based on the density gradient on the vibrating inclined deck. Due to the effect of inclined deck vibration, vertically separated particle layers into a horizontal separation from the feed section to the discharge end and particles are collected from specified portions based on the density difference.
In US5071541, a process for sorting plastic blasting media (PBM) used for stripping paint on surfaces, from a mixture of particles containing the same size and different in density like metal chips, sand and glass etc is given. The mixture of particles was supplied to a fluidized bed reservoir at one end such that the particles of the mixture settle at different levels in the reservoir in accordance with their density while moving towards another end of the reservoir collection point. The bottom wall of the reservoir is a diffusion membrane which defines an air manifold or plenum with the bottom wall.
In CN110293056A, a process for complete sorting of mined minerals with gas-solid fluidized bed dry separation technique using separating density gradient, coarse granule and fine grained are chosen as a separating medium particle is given. The coarse granules to fine grained size ratio not more than 10. Initially coarse granules and fine grained are kept completely separate condition. Under the action of airflow, the coarse granules and fine-grained granules start to fluidize and form high density sorting area, intermediate sort area and low-density sorting area. After the addition of sorting mined material from the top portion, it starts move from low density to high density sorting areas based on the density of the particles.
CN106622965B provides a process for mineral step dry method dense medium separation in a fluidized bed using medium solid of three kinds of different densities in the same sorting, it is adjusted in column body that generates three kinds of separating densities, can sort and obtain six kinds of products. The fluidized bed for separation is made of three-stage step cylinders connected with cone-type junction and the internal diameter of the cylinder section decreases from top to bottom. It includes sub material baffle located at the centre of the fluidized bed for separation sorting cylinder and circular cone connecter. The middle part of the two sections of the cylinder connection is equipped with a sub-material baffle made of two pieces of double-deck rectangle steel iron plates to separate the device into three sections for separation.
EP0377563A4 relates to a method for separating the mixture of agricultural products from associated waste materials using the inclined fluidized bed by forcing air upwardly through the fluidization medium. Here fluidization medium which is having the intermediate density of sink and float mixture of the solid mixture and the particle size of the fluidization medium must be smaller by several orders and the size of the articles contained in the mixture.
It is clear from the prior art that different methods have been employed to separate particles of different densities. However, there is a need for a specifically designed method and a specifically designed apparatus for separating low coke content catalyst from high coke content heel catalyst of continuous catalytic reforming (CCR) process which could be reutilized in CCR during normal operation and leads to the inventory cost saving in terms of fresh catalyst.
SUMMARY OF THE INVENTION
This summary is provided to introduce a selection of concepts, in a simplified format, that are further described in the detailed description of the invention. This summary is neither intended to identify key or essential inventive concepts of the invention and nor is it intended to determine the scope of the invention.
Accordingly, the present invention provides, a rotating fluidization method for separating a reusable low coke content catalyst from a high coke content heel catalyst of continuous catalytic reforming (CCR) process using a rotating fluidization column based on particle density gradient, the method comprising of: filling a fluidization column with heel catalyst; fluidizing using a gaseous fluidizing medium in upward direction; rotating the fluidization column axially across vertical axis which suppress the bubbles formation during fluidization; carrying out the fluidization of the catalyst in conjunction with column rotation for sufficient time in the range of 20-60 minutes preferably 30-40 minutes to ensure segregation of the catalyst particles and, removing catalyst sequentially from top to bottom bed after analysing the coke content, wherein, the bed height of heel catalyst is 0.3-0.7 times of the height of the fluidization column preferably 0.4-0.6 times of the height of the fluidization column.
The lower density catalyst particles with lower coke content move upward and higher density catalyst particles with higher coke content move downward and towards the circumference in the fluidization column and get stratified into different fractions based on the density gradient.
In an aspect the present invention provides, the coke content of the heel catalyst is 10-50 wt% preferably in the range of 15-45 wt%, and the average particle density of the heel catalyst is 1-2.5 g/cc preferably in the range of 1.3-2.2 g/cc.
In another aspect the present invention provides, the fluidizing medium is selected from air or nitrogen gas, wherein the superficial velocity of the fluidizing medium is 0.5-1.2 m/sec preferably 0.6-0.9 m/sec.
In another aspect the present invention provides, the rotational speed of the fluidization column is 30-150 rpm preferably in the range of 50-100 rpm.
In another aspect the present invention provides, the coke content of low coke content catalyst in the range of 0.1-10 wt%, and the average particle density of the coke content of low coke content catalyst is 1-1.3 g/cc.
The present invention also provides, a fluidization column apparatus for separating a reusable low coke content catalyst from a high coke content heel catalyst of continuous catalytic reforming (CCR) process, wherein the apparatus comprises of; a catalyst feed hopper (1) at top of the fluidization column; an inlet line with rotameter (2) for entering fluidizing medium at bottom of the fluidization column; a distributor (3) at bottom of the fluidization column; a column of multiple removable/insertable cylindrical columns sections, lower (4), middle (5) and upper (6); a flange connection (7) to connect the multiple removable/insertable cylindrical columns sections; a variable gear motor (8) attached through the gear assembly to rotate the fluidization column across vertical axis; an outlet line (9) located at top of column for the exit of fluidizing medium; a strainer (10) fitted inside the outlet line to avoid carryover of any catalyst particles; a collection point (13) located at the periphery of the fluidization column and closed with screw caps during normal operation; an aeration points (14) to avoid choking during the catalyst removal; a collection chamber (16) located at bottom portion of the fluidization column; and a collection point (17) at bottom of the fluidization column to collect the stratified catalyst.
In an aspect the present invention provides, the distributor is selected from the perforated plate or spider web.
In an aspect the present invention provides, a polymer mesh plate having an opening mesh size of 10-20 times the particle size of the catalyst to avoid the attrition of particles, is located at intermediate locations of cylindrical columns sections.
OBJECTIVES OF THE PRESENT INVENTION
The primary objective of the present invention is to provide a method for separating reusable low coke content catalyst from the heel catalyst having high coke content generated in continuous catalytic reforming (CCR) process based on the particle density gradient.
Another objective of the present invention is to provide a fluidization column apparatus for separating reusable low coke content catalyst from the heel catalyst having high coke content generated in continuous catalytic reforming (CCR) process.
BRIEF DESCRIPTION OF THE DRAWINGS:

Fig. 1: A schematic representation of the method and apparatus for separation of reusable catalyst from the heel catalyst using rotating fluidization column.
Fig. 2: A schematic representation of the method and apparatus for separation of reusable catalyst from the heel catalyst using rotating fluidization column with catalyst collection chamber.

ABBREVIATIONS
CCR: continuous catalytic reforming

DETAILED DESCRIPTION OF THE INVENTION
For the purpose of promoting an understanding of the principles of the invention, reference will now be made to the embodiments in the specific language will be used to describe the same. It will nevertheless be understood that no limitation of the scope of the invention is thereby intended, such alterations and further modifications in the illustrated process, and such further applications of the principles of the invention as illustrated therein being contemplated as would normally occur to one skilled in the art to which the invention relates. Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skilled in the art to which this invention belongs. The composition, methods, and examples provided herein are illustrative only and not intended to be limiting.
The articles “a”, “an” and “the” are used to refer to one or to more than one (i.e., to at least one) of the grammatical object of the article.
The terms “comprise” and “comprising” are used in the inclusive, open sense, meaning that additional elements may be included. It is not intended to be construed as “consists of only”.
Throughout this specification, unless the context requires otherwise the word “comprise”, and variations such as “comprises” and “comprising”, will be understood to imply the inclusion of a stated element or step or group of element or steps but not the exclusion of any other element or step or group of element or steps.
Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs. Although any methods and materials similar or equivalent to those described herein can be used in the practice or testing of the disclosure, the preferred methods and materials are now described. All publications mentioned herein are incorporated herein by reference.
The terminology and structure employed herein is for describing, teaching, and illuminating some embodiments and their specific features and elements and does not limit, restrict, or reduce the spirit and scope of the invention.
The CCR heel catalyst is high coke content catalyst recovered during the shutdown which is usually discarded and sent for precious metal recovery. However, the heel catalyst also contains some amount of low coke content catalyst which can be reused during normal CCR operation. The heel catalyst samples containing average coke content in the range of 10-50 wt%.
In a preferred feature, the heel catalyst samples contain the average coke content in the range of 15-45 wt%. The catalyst containing coke content in the range of 0.1-10 wt% can be separated from the heel catalyst based on density gradient using the fluidization technique in combination with the axial rotation of the column. The catalyst thus separated with 0.1-10 wt% coke content can be re-used in CCR process during normal operation. In one of the features of the present invention, the coke content of separated low coke content catalyst is in the range of 0.1 to 10 wt%.
The present invention provides a method of separating reusable low coke catalyst from the heel catalyst using rotating fluidization. To separate the reusable catalyst from the heel catalyst sample, the column is filled with the heel catalyst and fluidized using a gaseous fluidizing medium such as air or nitrogen gas. The fluidizing medium is passed through the bed in an upward direction to fluidize the catalyst particles. Additionally, the column is rotated axially across the vertical axis. The rotation of the column is applied by a variable gear motor connected to the column.
The low-density catalyst particles move upward while the high-density catalyst particles move downwards based on the density gradient under the influence of fluidization condition. The present invention also includes the axial rotation of the column across the vertical axis. The high-density catalyst particle moves towards the circumference compared to the low-density particles. Thus, improving the separation efficiency compared to conventional fluidization. Further, the axial rotation of the column across the vertical axis also suppresses the bubbles/slugs formation in the fluidization column and maintains uniform fluidization across the column which also improves the separation efficiency. The column is made up of multiple cylindrical columns to have the flexibility to change the fluidization column height. After completion of fluidization, catalyst samples can be separated either through the collection points provided at the periphery of the column or by disconnecting multiple cylindrical columns from top to bottom based on the density gradient of the catalyst bed in the column.
The present invention also provides a fluidization column apparatus for the separation of reusable catalyst from heel catalyst as indicated in Fig.1, the catalyst sample charged in the column through the catalyst feed hopper (1). The column should be filled in a way such that the bed height is 0.3-0.7 times of the height of the fluidization column as the catalyst bed expands during fluidization. In a preferred feature, bed height is 0.4-0.6 times of the height of the fluidization column. The column is made of three sections joined through flange connections (7); lower (4), middle (5) and upper (6) cylindrical sections. The fluidizing medium such as air or nitrogen gas passes through the inlet line with a rotameter (2) and enters the bottom section (4) through a distributor (3) such as a perforated plate or spider web for fluidization of the catalyst bed present in the column. The column is rotated through the variable gear motor (8) attached through the gear assembly. The catalyst particles get stratified into different fractions under the combined effect of fluidization and rotation of the column. The fluidizing medium such as air or nitrogen gas exit through the outlet line (9) located at the top of the column and fitted with a strainer (10) to avoid carryover of any catalyst particles. The column is also containing mesh plates (11) at intermediate locations. After fluidization of the catalyst is carried out for a sufficient time in the range of 20-60 min, preferably 30-40 min, the rotation of the column and the flow of the fluidizing medium is stopped. The catalyst bed is stratified as per the density and thereby according to the coke content. The top layer of the bed (12) which contains low coke catalyst particles is removed through the collection point (13) located at the periphery of the column and closed with screw caps during normal operation. The collection points are equipped with aeration points (14) to avoid choking during the catalyst removal. Since it is difficult to establish the layer thickness to ensure the coke content is in the range of 0.1-10 wt%, the sample collection points are located at various heights. The number of sample collection points may be higher in the middle section and lesser in the lower section. The catalyst is removed sequentially from the top to bottom bed (15) after analysing the coke content.
According to Fig. 2, for separation of reusable catalyst from the heel catalyst, after completion of fluidization, catalyst samples can be separated by disconnecting multiple cylindrical columns from top to bottom based on the density gradient of the catalyst bed and catalyst samples collected in catalyst collection chamber (16) located at the bottom portion of the column and later catalyst collected through catalyst collection points (17). The catalyst collection chamber (16) is assembled at bottom of the column (4) after the completion of fluidization.
In one feature of the present invention the polymer mesh plates have an opening mesh size of about 10-20 times the particle size to avoid the attrition of particles. The mesh plates placed at every cylinder junction help to overcome the discontinuous passageways or bubble formation in the fluidization and help uniform fluidization across the column.
The present invention provides, a rotating fluidization method and a fluidization column apparatus for efficient recovery of low coke content catalyst having average particle density around 1-1.3 g/cc from the CCR heel catalyst sample having average particle density around 1-2.5 g/cc using fluidization technique based on the density gradient. In a preferred feature, the CCR heel catalyst sample has the average particle density in the range of 1.3-2.2 g/cc. The density of the catalyst increases with the coke content. A substantial density difference is observed between the catalyst having 0.1-10 wt% coke content and the catalyst having coke content more than 10 wt% (up to 50 wt%) coke content. This density difference is the premise for the separation under the combined effect of rotation and fluidization forces in a rotating fluidization column.
In one feature of the present invention, the desired separation of low coke content catalyst is achieved in a rotating fluidization column operating using air or nitrogen gas with the superficial velocity in the range of 0.5-1.2 m/sec preferably 0.6-0.9 m/sec and the column rotational speed in the range of 30-150 rpm. In a preferred feature, superficial velocity is in the range of 0.6-0.9 m/sec and the column rotational speed in the range of 50-100 rpm. The apparatus is also flexible for operating different quantities of catalyst samples.
In another feature of the present invention, after the completion of fluidization, the catalyst sample is segregated into top and bottom portions separately. The top and bottom portions of the composite catalyst samples are analyzed individually for coke content in the carbon analyzer. Prior to the analysis, catalyst samples were calcined in the range of 170-200 ? for at least 2 hrs to remove any moisture and hydrocarbons present in them and catalyst samples were further crushed into fine powder. Around 0.1-0.5 g of sample is analyzed in the carbon analyzer along with accelerators like tungsten and iron for complete combustion of coke material present in the catalyst sample in an oxygen environment. During the combustion, carbon is converted into a mixture of carbon monoxide (CO) and carbon dioxide (CO2) and CO is further oxidized to CO2. The emitted CO2 content is detected by infrared cells and back-calculated for carbon content deposited on the catalyst.
In the present method, the combined effect of rotational and fluidization forces improves the separation efficiency in comparison to conventional fluidization. Further, the rotating column suppresses the formation of bubbles in the column and maintains uniform fluidization.
The present invention does not require the use of any non-transitory or transitory foreign coarse particles or intermediate density particles in the system for the separation of catalyst samples based on the density gradient.

EXAMPLES:
The present disclosure with reference to the accompanying examples describes the present invention. However, those of skill in the art should, in light of the present disclosure, appreciate that many changes can be made in the specific embodiments which are disclosed and still obtain a like or similar result without departing from the spirit and scope of the invention. It is understood that the examples are provided for the purpose of illustrating the invention only and are not intended to limit the scope of the invention in any way.
Example 1: In this example, experiments 1-2 were conducted with a heel catalyst sample having coke content 19.92 wt% using disclosed method and apparatus, to study the effect of rotation of the column. The median diameter of the heel catalyst samples used is 1.8 mm. In Exp. No. 1, the catalyst bed was fluidized using air at a superficial velocity of 0.8 m/sec for 30 min keeping the column at static condition. In Exp. No. 2, the column was rotated at a speed of 60 rpm with the help of a variable gear motor connected to the column. In these experiments 1-2, the catalyst bed was separated into equal portions top and bottom. The results are tabulated below in Table-1
Table-1: Experimental data of separation of low coke content catalyst from heel catalyst Sample-A
Exp. No. Heel catalyst Average coke content, wt% Column condition Average coke content of catalyst after fluidization, wt% Recovered catalyst after fluidization, wt%
1 Sample-A 19.92 Static 9.90 50
28.02 50
2 Rotation 5.62 50
29.29 50

It is evident from the above experimental result as given in Table-1, that heel catalyst samples are effectively separated based on density gradient using the disclosed method and apparatus.
Example 2: In this example, the heel catalyst sample with a median diameter of 1.8 mm and average coke content of 18.15 wt% was separated using disclosed method and apparatus. The catalyst bed was fluidized using air for 30 min with the column rotating at a speed of 90 rpm with the help of a variable gear motor connected to the column. Experiments 3-5 were conducted with different superficial velocities of air in the range of 0.6-1 m/sec as given in Table-2. In these experiments, the top bed comprising of 45 wt% catalyst with low coke content was separated. The remaining 55 wt% of catalyst remained in the bottom bed with high coke content was collected separately from the bottom of the column. Both low and heavy coke content fractions were tested for the average coke content in it. The results are tabulated as shown below Table-2.
Table-2: Experimental data of separation of low coke content catalyst from heel catalyst with Samples-B at different superficial velocities in the range of 0.6-1 m/sec
Exp. No. Heel catalyst Average coke content, wt% Superficial velocity, m/sec Average coke content after separation, wt% Recovered catalyst after fluidization, wt%
3 Sample-B 18.15 0.6 11.54 45
22.44 55
4 0.8 8.93 45
25.79 55
5 1.0 17.68 45
20.30 55

From these experimental results as given in Table-2, better separation was achieved at a superficial velocity of 0.8 m/sec. At a higher superficial velocity of 1 m/sec, the separation of low coke content catalyst was found to be low. This may be attributed to the predominance of catalyst particles back mixing across the column instead of stratification based on the density gradient.
Example 3: In this example, experiments were conducted with various heel catalyst samples having coke content in the range of 14-32 wt%, as given in Table-3, using disclosed method and apparatus. The median diameter of the heel catalyst samples used is 1.8 mm. The catalyst bed was fluidized using air at a superficial velocity of 0.8 m/sec with the column rotating at a speed of 90 rpm with the help of a variable gear motor connected to the column. In these experiments, the low coke content catalyst having 0.1-10 wt% coke is separated from the heel catalyst samples. The results are tabulated as shown below in Table-3.
Table-3: Experimental data of separation of low coke content catalyst from heel catalyst Samples C – F
Exp. No. Heel catalyst
Average coke content, wt% Average coke content after separation, wt% Recovered catalyst after fluidization, wt%
6 Sample-C 22.64 <10 19.0
27.0 81.0
7 Sample-D 30.52 <10 14.0
32.5 86.0
8 Sample-E 31.98 <10 12.2
29.9 87.8
9 Sample-F 13.86 <10 57.0
33.0 43.0
It is evident from the above Table-3 that a low coke content catalyst is in the range of 12-57 wt% was recovered from actual heel catalyst samples using the disclosed method and apparatus. These recovered catalysts can be reused in existing CCR operation and lead to substantial saving in terms of the cost of fresh catalyst.
Advantages of the present invention
The present invention provides a method and apparatus for a separation process for recovery of reusable low coke content catalyst from the heel catalyst sample.
The advantage of the present invention is easy to separate reusable low coke catalyst from the heel catalyst sample in a rotating fluidization column with the superficial velocity of fluidizing medium in the range of 0.5-1.2 m/sec preferably 0.6-0.9 m/sec and rotational speed is in the range of 30-150 rpm, preferably in the range of 50-100 rpm. During the fluidization, the heel catalyst fluidizes under the action of air or nitrogen gas upward flow and gets stratified into different fractions based on density gradient. The lighter particles move upward, and heavier particle moves downward of the column. The particles separated after the completion of the fluidization for the desired time.
Another advantage of the present invention is to provide the apparatus for handling different quantities of catalyst for separation of reusable low coke catalyst from heel catalyst with changing the height of the fluidization column by addition or removal of cylindrical columns from the existing column. The catalyst samples can be easily collected or separated by disconnecting cylindrical columns from top to bottom from the existing column after the completion of fluidization.
Another advantage of the present invention is along with fluidization, the rotation of the column improves the separation efficiency compared to conventional fluidization. The rotation of the column suppresses the formation of the bubbles and helps in maintaining uniform fluidization across the column.
Yet another advantage of the present invention is the recovery of a substantial amount of the low coke content catalyst which will reduce inventory cost in terms of fresh catalyst. , Claims:1. A rotating fluidization method for separating a reusable low coke content catalyst from a high coke content heel catalyst of a continuous catalytic reforming (CCR) process using a rotating fluidization column based on the particle density gradient, wherein the method comprising the steps of:
- filling a fluidization column with the heel catalyst;
- fluidizing using a gaseous fluidizing medium in an upward direction;
- rotating the fluidization column axially across the vertical axis which suppresses the formation of the bubbles during fluidization; and
- removing catalyst sequentially from top to bottom bed after analysing the coke content,
wherein, the bed height of the heel catalyst is 0.3-0.7 times the height of the fluidization column, preferably 0.4-0.6 times the height of the fluidization column;
the lower density catalyst particles with lower coke content move upward and higher density catalyst particles with higher coke content move downward and towards the circumference in the fluidization column and get stratified into different fractions based on the density gradient.

2. The method as claimed in claim 1, wherein the coke content of the high coke content heel catalyst is in the range of 10-50 wt%, preferably in the range of 15-45 wt%.

3. The method as claimed in claim 1, wherein an average particle density of the high coke content heel catalyst is in the range of 1-2.5 g/cc, preferably in the range of 1.3-2.2 g/cc.

4. The method as claimed in claim 1, wherein the fluidizing medium is selected from air or nitrogen gas.

5. The method as claimed in claim 1, wherein the fluidizing medium is moving with a superficial velocity in the range of 0.5-1.2 m/sec, preferably 0.6-0.9 m/sec.

6. The method as claimed in claim 1, wherein the fluidization column is rotated at a rotational speed of 30-150 rpm, preferably in the range of 50-100 rpm.

7. The method as claimed in claim 1, wherein the coke content of low coke content catalyst in the range of 0.1-10 wt%, and the average particle density of the low coke content catalyst is in the range of 1-1.3 g/cc.

8. A fluidization column apparatus for separating a reusable low coke content catalyst from the heel catalyst having high coke content generated in the continuous catalytic reforming (CCR) process, wherein the apparatus comprises of:
-a catalyst feed hopper (1) at top of the fluidization column;
-an inlet line with rotameter (2) for entering fluidizing medium at bottom of the fluidization column;
-a distributor (3) at bottom of the fluidization column;
-a column of multiple removable/insertable cylindrical columns sections, lower (4), middle (5) and upper (6);
-a flange connection (7) to connect the multiple removable/insertable cylindrical columns sections;
-a variable gear motor (8) attached through a gear assembly to rotate the fluidization column across the vertical axis;
-an outlet line (9) located at top of the fluidization column for the exit of the fluidizing medium;
-a strainer (10) fitted inside the outlet line to avoid carryover of any catalyst particles;
-a collection point (13) located at the periphery of the fluidization column and closed with screw caps during normal operation;
- aeration points (14) to avoid choking during the catalyst removal;
-a collection chamber (16) located at the bottom portion of the fluidization column; and
-a collection points (17) at bottom of the fluidization column to collect stratified catalyst.

9. The fluidization column apparatus as claimed in claim 8, wherein the distributor is selected from the perforated plate or spider web.

10. The fluidization column apparatus as claimed in claim 8, wherein a polymer mesh plate (11) having an opening mesh size of 10-20 times the particle size of the catalyst to avoid the attrition of particles, is located at intermediate locations of the cylindrical column sections